CN105004141B - 液化富烃馏分的方法 - Google Patents

液化富烃馏分的方法 Download PDF

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CN105004141B
CN105004141B CN201510296586.5A CN201510296586A CN105004141B CN 105004141 B CN105004141 B CN 105004141B CN 201510296586 A CN201510296586 A CN 201510296586A CN 105004141 B CN105004141 B CN 105004141B
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B·海因茨
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Abstract

本发明描述一种用于液化和过冷富烃馏分特别是天然气的方法，一旦冷却，馏分被部分冷凝以除去重质烃类，特别是苯。根据本发明，a)已液化的富烃馏分(7)在单独的换热器(E3)中被过冷(标准模式)，b)最迟在达到换热器(E3)中限定的固体沉积值时，中断向换热器(E3)供应已液化的富烃馏分(7)(清洗模式)，c)在换热器(E3)中的固体通过融霜气体(10、11)融化并且从换热器(E3)排出，和d)已液化的富烃馏分(7)随后回到换热器(E3)。

Description

液化富烃馏分的方法
技术领域
本发明涉及一种用于液化和过冷富烃馏分、特别是天然气的方法，其中一旦冷却，所述馏分被部分冷凝以除去重质烃类，特别是苯。
背景技术
富烃馏分的液化和过冷通常相逆于至少一个制冷剂循环和/或至少一个混合制冷剂循环而实现。
在富烃馏分、特别是天然气的液化中，防止由待液化馏分的某些成分的冻结所引起的停机是非常重要的。在外界温度下，在开始加工时，通常通过化学清洗(例如胺洗涤)和/或吸附法将水和二氧化碳去除至一定程度，从而在富烃馏分的液化期间它们不会产生不希望的固体形式。
易于冻结的重质烃类(HH)(在下文中术语“重质烃类”包含C6+烃类)，特别是苯，在环境条件下，仅在很高成本和不便的情况下才能从待液化的馏分中除去。因此通常的做法是使进气进行少量部分的冷凝，然后在分离器中排出富HH液态馏分，以便充分地降低由该分离器排出的气相将在随后的液化和过冷期间冻结的风险。
然而，部分冷凝通常仅仅保证当待液化的气体混合物包括具有中间沸程的成分，例如丙烷、丁烷和/或戊烷时，HH、特别是苯在气相中是十分贫瘠的，所述具有中间沸程的成分在进气冷却期间在HH之前以充足的数量进行液化，并且由此作为所述HH的溶剂。
当在进气成分中的中间沸化物-称为所谓的贫气-浓度不足时，其不能通过部分冷凝以及随后富HH液体的去除来充分消耗苯(通常是<1ppmv)，仍然会发生不必要的冻结。
发明内容
本发明的目的是详细说明一种所讨论类型的液化和过冷富烃馏分、特别是天然气的方法，即使在这些条件下，其也能实现可靠并且经济地去除重质烃类。
该目的是通过液化和过冷富烃馏、特别是天然气的方法而实现的，所述方法的特征在于：
a)已液化的富烃馏分在单独的换热器中过冷(标准模式)，
b)最迟在达到换热器中限定的固体沉积值时，中断向换热器供应已液化的富烃馏分(清洗模式)，
c)在换热器中的固体用融霜气体融化并从换热器中排出，和
d)已液化的富烃馏分随后回到换热器中。
根据本发明，已液化的富烃馏分现在在单独的换热器(再冷却器)中过冷，其中有意地允许固体的冻结或沉积。由此方法有意地设法在-70℃温度以下，优选地在-80℃以下，在天然气液化的再冷却器中得到重质烃类的固体形式。当已经达到在该单独的换热器中限定的固体沉积值时，标准模式中断并且该方法转换到清洗模式。为了实现这种情况，中断向再冷却器供应待过冷的已液化富烃馏分，并且已液化的馏分被立即送至用于其他使用和/或中间储存器。上述限定的固体沉积值例如可以通过在经过再冷却器期间待过冷的富烃馏分的压降增加而确定。根据本发明，清洗模式包括使用适量融霜气体在合适的温度融化固体，并且随后在合适的点、优选地在一个或多个管道低点，从单独的换热器中排出融化产物，并且通常以浓缩的形式将所述融化的固体送到工厂范围以外。选择融霜气体的量和/或温度以使至少50％，优选地至少70％的固体量可以被融化和除去。根据本发明展开的方法建议一旦在单独的换热器中的固体已经融化，使用气态或液态清洁介质清洁至少其中形成固体的单独的换热器的换热器通道。该清洁融化并除去余留在单独的换热器中的固体。特别合适的清洁介质是干氮以及在液化和过冷富烃馏分的中间储存期间产生的蒸发气态馏分。
在清洗之后，终止融霜气体和/或清洁介质的供应，并且通过待过冷的已液化富烃馏分返回到单独的换热器而将方法转变成标准模式。
当在标准模式时，已液化的富烃馏分在单独的换热器中相逆于至少一个制冷剂流和/或至少一个混合制冷剂流而被过冷，根据本发明用于液化和过冷富烃馏分的方法的一个有益的实施方案的特征在于在清洗模式下使用这种制冷剂流和/或混合制冷剂流来冷却待液化的富烃馏分。
由于在清洗模式的制冷剂流和/或混合制冷剂流的上述改变流路，布置在单独的换热器上游的换热器或换热器区域至少在一定程度上承担所述单独的换热器的过冷功能。该方式有效地避免以下情况，在清洗模式中由液化区域排出的已液化的富烃馏分明显地比在标准模式下由单独的换热器排出的过冷馏分更热。因此即使在清洗模式，在该工艺的冷端排出的已液化的富烃馏分的温度至多为30℃，优选地至多为20℃，比在标准模式中已过冷的富烃馏分的温度更高。
当待液化的富烃馏分相逆于至少一个制冷循环液化和过冷时，根据本发明方法的其他有益的实施方案是清洗模式需要的融霜气体是在制冷循环中循环的制冷剂的支流。当该制冷循环包括例如两级压缩机单元时，作为融霜气体的制冷剂支流可以从第二压缩机级的吸入侧排出，膨胀到合适的压力并且选择性地被加热，由所述单独的换热器中通过并且随后送到第一压缩机级的吸入侧。
附图说明
根据本发明用于液化和过冷富烃馏分的方法，以及其其他有益的实施方案参考图1和2示出的工作实施例而在下文更特别地说明。
图1示出了富烃馏分相逆于混合循环被液化和过冷的方式，而图2示出两级氮膨胀器循环的实施方式。
具体实施方式
待液化的富烃供给馏分1，例如所谓的贫化天然气，在实际液化之前送到去除单元A，在该去除单元中使用化学洗涤和/或吸附方法来除去水和二氧化碳，并通过线路2将它们排出。由此预纯化的供给馏分3被送到第一换热器或换热器区域E1，其在此被冷却并且部分地冷凝。部分冷凝的馏分4然后被送到分离器D1，并且分离成包含重质烃类的液态馏分5和富烃气态馏分6。前者从分离器D1的底部通过控制阀V6排出时，而气态馏分6在第二换热器或换热器区域E2中被液化。根据本发明，已液化的富烃馏分7在单独的换热器或再冷却器E3中被过冷。已过冷的富烃馏分8——在天然气LNG产品馏分的情况下——通过阀V4输送至用于其他使用和/或至中间储存器。上面描述的换热器E1到E3可以是螺旋形盘管换热器和/或焊接板式换热器。
在图1示出的方式中，相逆于包括两级压缩机单元C1的混合循环而实现富烃馏分的冷却、液化和过冷。在换热器E1到E3中的蒸发和加热的制冷剂通过线路20送到布置在压缩机单元C1第一级上游的容器D2。积聚在所述容器中的气态馏分21在压缩机单元C1的第一压缩机级中被压缩到中间压力，在中间冷却器E4中冷却和部分冷凝，然后通过线路22送到第二分离器D3。积聚在所述第二分离器中的气态馏分23在压缩机单元C1的第二压缩机级被压缩到所希望的最终循环压力，然后通过其中布置有后冷却器E5的线路27送到第三分离器D4。
从第二分离器D3底部排出的液态馏分25在换热器E1中冷却。该馏分随后在阀V1中制冷膨胀，并且通过线路26与待冷却的富烃供给馏分3反向地经过换热器E1。当积聚在第三分离器D4中的液态馏分28通过控制阀V5被回收到第二分离器D3的上游点时，积聚在第三分离器D4中的气态馏分29同样被冷却并且在换热器E1中部分冷凝，然后在分离器D5中分离成液态馏分30和气态馏分32。
后者在换热器E2和E3中冷凝和过冷，在阀V3中进行制冷膨胀，然后经线路33由单独的换热器E3通过以提供在其中需要的最大制冷。该馏分随后通过控制阀V7和线路34与在换热器E2中冷却的液态馏分30混合。所述液态馏分在膨胀阀V2中进行制冷膨胀，并且随后经线路31与待冷却和液化的富烃供给馏分3/6反向地由换热器E2和E3中通过。
根据本发明，换热器或再冷却器E3是独立的装置。所述装置仅仅通过管道连接到换热器E1和E2。此时，当达到在换热器E3中限定的固体沉积值时，所述工艺从标准模式转换到清洗模式。这通过关闭阀V4和打开阀V9实现，所以液化的富烃馏分7通过线路9绕过换热器E3。同时，控制阀V3和V7关闭并且阀V8打开，所以从分离器D5排出的气态馏分32此时仅仅经过换热器E2。由于制冷剂馏分32的这种改变流路，换热器E2至少在一定程度上承担已液化的富烃馏分的过冷，其在单独的换热器E3中在标准模式下是有效果的。
随着上述阀V3、V4和V7到V9的打开和关闭，以及阀V10和V11打开，合适温度以及合适量的融霜气体同时经线路10由换热器E3中通过，然后经线路11排出。设置在线路10中的换热器E6加热该融霜气体。此时，不是在标准模式下流经换热器E3的制冷剂馏分32，而是融霜气体10作为传热介质并且融化沉积在换热器E3中的固体。所述固体可以在换热器E2和E3之间的合适点例如在管道低点，通过适当的截止阀以浓缩的形式被排出，为了清楚而没有示出该截止阀。
在图2示出的方式中，富烃供给馏分的冷却、液化和过冷通过两级氮膨胀器循环而实现。由于这里的用于待液化和过冷的富烃供给馏分的方式和图1的相同，因此不会另外在下文中论述；因此下列描述的仅仅是氮膨胀器循环。
在换热器E1到E3中加热的富氮制冷剂40在压缩机单元C1′的第一压缩机级压缩到中间压力，在中间冷却器E4′中冷却，并且通过线路41送到压缩机单元C1′的第二压缩机级中。压缩到循环端压力的制冷剂42在后冷却器E5′中被冷却，并且在换热器E1和E2中被冷却。冷却的制冷剂的第一支流43被送到第一膨胀器X1，在其中进行制冷和做工膨胀，并且经线路44与待液化的富烃供给馏分3反向地由换热器E2和E1中通过。第二制冷剂支流45被送到第二膨胀器X2，同样进行制冷和做工膨胀，经线路46与待过冷的富烃馏分7反向地由单独的换热器E3中通过，并且随后通过阀V7′与上述制冷剂支流44混合。
当达到换热器X3中限定的固体沉积值时，第二膨胀器X2排出流。同时操作阀V7′关闭和阀V8′、V10′和V11′打开。随着阀V8′打开，已经送到第二膨胀器X2的第二制冷剂支流45此时通过线路52输送到第一膨胀器X1的上游点，所述线路52在图中以虚线示出。随着阀V10′打开，所述阀用于调节所希望的融霜气体压力，从第二压缩机级上游排出的制冷剂支流作为融霜气体通过线路50被送到换热器E3，所述线路50在图中以虚线示出。换热器E6′用于任何融霜气体的加热需要。已经经过换热器E3，并且随着阀V11′打开，融霜气体通过线路51回收到压缩机单元C1′的第一压缩机级的上游点，所述线路51在图中用虚线示出。
根据本发明的用于液化和过冷富烃馏分特别是天然气的方法，在即使使用所谓的贫气时，也能实现可靠地和经济地去除重质烃类，特别是苯。根据本发明理念的实施并不依赖所选择的富烃馏分的液化和过冷的类型。

Claims (7)

1.一种用于液化和过冷富烃馏分的方法，其中该方法包括以下步骤：
a)提供富烃馏分(3)；
b)在第一换热器(E1)中冷却该富烃馏分(3)，以形成部分冷凝的馏分(4)；
c)分离该部分冷凝的馏分(4)，以形成包含重质烃类的液体馏分(5)和富烃气体馏分(6)；
d)在另一个换热器(E2)中液化所述富烃气体馏分(6)，以形成已液化的富烃馏分(7)；
其中所述方法还包括：
e)在标准模式下运行，其包括：
e1)所述已液化的富烃馏分(7)在单独的换热器(E3)中被过冷，以产生过冷的富烃馏分(8)；
e2)监测在所述单独的换热器(E3)中形成的固体沉积的量；
f)当固体沉积的量达到限定值时，在清洗模式下运行，其包括：
f1)中断向所述单独的换热器(E3)中供应已液化的富烃馏分(7)；
f2)向所述单独的换热器(E3)中送入融霜气体，由此融化所述固体沉积；
f3)从所述单独的换热器(E3)中排出已融化的沉积；和
g)随后返回标准模式下的运行，其中所述已液化的富烃馏分(7)被送入所述单独的换热器(E3)中以过冷。
2.根据权利要求1的方法，其中
在标准模式下的步骤e)中，所述已液化的富烃馏分(7)在所述单独的换热器(E3)中相逆于至少一个制冷剂流和/或至少一个混合制冷剂流而被过冷，以及
在清洗模式下的步骤f)中，所述制冷剂流和/或所述混合制冷剂流还被用来在第一换热器(E1)和/或所述另一个换热器(E2)中冷却所述富烃馏分。
3.根据权利要求1的方法，其中在步骤b)和d)中，所述富烃馏分相逆于至少一个制冷循环被液化和过冷，该制冷循环具有制冷剂，其中该制冷剂的支流是所述融霜气体。
4.根据权利要求1至3中任一项的方法，其中步骤f)中的所述清洗模式进一步包括：在所述单独的换热器(E3)中的固体沉积已被融化后，清洁其中发生所述固体沉积的所述单独的换热器(E3)的通道。
5.根据权利要求4的方法，其中
所述过冷的富烃馏分(8)被送入中间储存；和
所述单独的换热器(E3)的通道是通过提供干氮和/或在所述过冷的富烃馏分(8)的中间储存期间产生的蒸发的气态馏分而被清洁的。
6.根据权利要求1至3中任一项的方法，其中所述富烃馏分的冷却、液化和过冷在螺旋形盘管换热器和/或焊接板换热器中进行。
7.根据权利要求1至3中任一项的方法，其中所述富烃馏分包括天然气。
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